Processing of lithium containing material

ABSTRACT

A process ( 10 ) for the treatment of a lithium containing material, the process comprising the steps of:
         (i) Preparing a process solution from the lithium containing material ( 12 );   (ii) Passing the process solution from step (i) to a series of impurity removal steps ( 36 ) thereby providing a substantially purified lithium chloride solution; and   (iii) Passing the purified lithium chloride solution of step (ii) to an electrolysis step ( 70 ) thereby producing a lithium hydroxide solution.

FIELD OF THE INVENTION

The present invention relates to the treatment of lithium containingmaterial.

More particularly, the present invention relates to a process for thetreatment of a lithium containing material and the production of lithiumhydroxide and lithium carbonate. The process utilising the electrolysisof a lithium chloride solution obtained from either a spodumene ore orconcentrate, or from brines. In one form, the process of the presentinvention is intended to provide a high purity or battery grade lithiumhydroxide and lithium carbonate product.

The process of the present invention may further provide a hydrochloricacid product. Still further, the process of the present invention, inone form, utilises precious metal containing mixed metal oxide (MMO)electrodes to heighten the efficiency of an electrochemical portion ofthe process.

BACKGROUND ART

Known processes for the production of lithium carbonate from lithiumcontaining ores or concentrates typically utilise the thermal treatmentof an alpha-spodumene ore or concentrate. This thermal treatment can bereferred as decrepitation and transforms the alpha-spodumene tobeta-spodumene which is in turn able to be solubilised by acid. The stepin which the beta-spodumene is solubilised in acid takes place in a kilnand produces soluble lithium salt. The lithium salt is passed to one ormore tanks in which the lithium salt is purified. Leached crude lithiumsalt is subsequently passed to a step in which the pH of the slurry isadjusted, whereby certain impurities, including iron and magnesium areintended to be precipitated. Thus purified lithium salt is treated withsoda ash to produce lithium carbonate. This lithium carbonate can befurther treated with hydrated lime to produce lithium hydroxide.

Processes for the production of lithium carbonate and lithium hydroxidefrom brines typically involves the use of evaporation ponds to increasethe concentration of the salts contained therein before being passed toa series of steps aimed to reduce the impurities present.

The above described processes of the prior art are relativelyinefficient in the removal of impurities remaining in the pregnant leachsolution, which results in a relatively impure lithium hydroxide andlithium carbonate product. This is particularly problematic whenattempting to produce high quality or battery grade lithium hydroxideand lithium carbonate products.

The process of the present invention has as one object thereof toovercome substantially one or more of the above mentioned problemsassociated with prior art processes, or to at least provide a usefulalternative thereto.

The preceding discussion of the background art is intended to facilitatean understanding of the present invention only. This discussion is notan acknowledgement or admission that any of the material referred to isor was part of the common general knowledge as at the priority date ofthe application.

Throughout the specification and claims, unless the context requiresotherwise, the word “comprise” or variations such as “comprises” or“comprising”, will be understood to imply the inclusion of a statedinteger or group of integers but not the exclusion of any other integeror group of integers.

The term “battery grade lithium carbonate” refers to a product having apurity of about 99.5% or higher. Similarly, the term “battery gradelithium hydroxide” refers to a product having a purity of about 99% orhigher.

Disclosure of the Invention

In accordance with the present invention there is provided a process forthe treatment of a lithium containing material, the process comprisingthe steps of:

-   -   (i) Preparing a process solution from the lithium containing        material;    -   (ii) Passing the process solution from step (i) to a series of        impurity removal steps thereby providing a substantially        purified lithium chloride solution; and    -   (iii) Passing the purified lithium chloride solution of        step (ii) to an electrolysis step thereby producing a lithium        hydroxide solution; and    -   (iv) Carbonating the lithium hydroxide solution produced in        step (iii) by passing compressed carbon dioxide through the        solution, thereby producing a lithium carbonate precipitate.

Wherein the lithium containing material is an alpha-spodumene ore or oreconcentrate and the process further comprises a first step in which thatalpha-spodumene ore or ore concentrate is calcinated to producebeta-spodumene.

In one form of the present invention, the process solution of step (i)is prepared in the form of a pregnant leach solution. Preferably, thepregnant leach solution is formed by passing a lithium containingmaterial to a leach step in which the material is leached withhydrochloric acid.

Preferably, the impurity removal step (ii) further comprises aconcentration step wherein the pregnant leach solution is concentratedto near saturation of lithium chloride.

The lithium hydroxide solution produced in step (iii) may be thickenedby evaporation of water to provide lithium hydroxide monohydratecrystals.

In a further form of the present invention a first portion of thelithium hydroxide solution produced in step (iii) is thickened byevaporation/crystallisation to provide lithium hydroxide monohydratecrystals and a second portion thereof is carbonated by passingcompressed carbon dioxide through the solution, thereby producing alithium carbonate precipitate.

Preferably, the impurity removal steps of step (ii) include one or moreof hyrdropyrolysis of Al and Fe chlorides, pH increase to precipitatehydroxides of Al, Fe, Mg and Mn, lithium carbonate precipitation forremoval of Ca, and fractional crystalisation for the removal of Na andK.

Still preferably, the fractional crystallisation for the removal of Naand K is conducted immediately after the concentration step.

The impurity removal steps preferably further comprises an ion exchangestep. Preferably, the ion exchange step removes substantially allcalcium, magnesium and other multivalent cations remaining in thepregnant leach solution. Still preferably, such multivalent cations areremoved to a level of less than about 10 ppm.

Still preferably, water evaporated from the solution inevaporation/crystallisation is recompressed, combined with make-up steamand utilised in evaporation/crystallisation. Theevaporation/crystallisation step preferably utilises a vacuumevaporative crystalliser.

Preferably, the beta-spodumene is cooled and milled prior to the leachstep. The beta-spodumene is preferably milled to less than about 300 μm.Still preferably, the beta-spodumene is milled to a P₈₀ of about 75 μm.

Preferably, the leach step is conducted at elevated temperature.

The hydrochloric acid solution used in the leach step is preferablyabout 20% HCl w/w.

Still preferably, the elevated temperature of the leach step is aboutthe boiling point of the hydrochloric acid solution used in the leachstep.

The leach step is preferably conducted at atmospheric pressure.

In one form of the present invention the leach step is conducted in achlorination kiln at about 108° C. over a residence time of about 6 to10 hours. Preferably, the residence time is about 8 hours.

BRIEF DESCRIPTION OF THE DRAWINGS

The process of the present invention will now be described, by way ofexample only, with reference to one embodiment thereof and theaccompanying drawing, in which:

FIG. 1 is a schematic flow-sheet depicting a process for the treatmentof a lithium containing material in accordance with a first embodimentof the present invention in which the lithium containing material is analpha-spodumene concentrate.

BEST MODE(S) FOR CARRYING OUT THE INVENTION

In FIG. 1 there is shown a process 10 for the treatment of a lithiumcontaining material in accordance with a first embodiment of the presentinvention in which embodiment the lithium containing material isprovided in the form of an alpha-spodumene concentrate.

All of the unit operations embodied in the process 10 are intended tooperate continuously with full process instrumentation and control beingprovided for.

An alpha-spodumene concentrate 12 is passed to a calcining step in whichthe concentrate 12 is calcined in a calcining furnace 14 at atemperature of between about 1050° C. to 1100° C. to convert thealpha-spodumene to leachable beta-spodumene. Off-gases from the calcinerare directed through a cyclone (not shown) and an electrostaticprecipitator (not shown) specified to comply with known environmentalemissions limits. The resulting hot calcine is passed to a cooler 16 andindirectly cooled to about 80° C. It is then dry-milled to less than 300μm, for example to a P₈₀ of about 75 μm, in a mill, for example a closedcircuit ball mill 18.

After storage in a surge bin (not shown), the milled beta-spodumene ismixed with at least a 40 to 300% stoichiometric excess of 20%hydrochloric acid w/w 20 in a slurrying step. The slurrying step feeds aleach step, for example a leach circuit 22, comprising a first leachstage 24 and a second leach stage 26.

The leach step is conducted at about 108° C., being the boiling point ofthe hydrochloric acid leach solution added in the slurrying step, for aperiod of about 6 to 12 hours, for example about 8 hours, in continuousleach tanks. A pulp density of about 40% is used in the leach circuit 22to maximise the leach concentration and to ensure that the solubilitylimit of lithium chloride during leaching is not exceeded. Off-gases arecleaned in a wet scrubber (not shown). The leach step 22 produces aresidue slurry and a process solution, for example a pregnant leachsolution. The lithium and the aluminosilicate in the beta-spodumeneleaches into solution with other impurities to give a sub-saturatedconcentration of lithium chloride in the pregnant leach liquor.

The pregnant leach solution from the leach circuit 22 is passed to athickening circuit 28, preferably comprising two stages 28 a and 28 baligned with the stages 24 and 26 of the leach circuit 22. An overflowfrom the thickening circuit 28 is directed to a pyrohydrolysis step 30,operating at about 300 oC, and in which chlorides of Al and Fe presentin the pregnant leach solution are converted into their respectiveinsoluble oxides 32. Any residual HCl is also recovered in an HCLremoval step 34.

In addition to the Al and Fe described immediately above as beingrecovered using the pyrohydrolysis step 30, remaining soluble iron,aluminium and magnesium are removed in large part from the leach liquorthrough a series of impurity removal steps, indicated in a broad senseby impurity removal steps 36 in FIG. 1. The impurity removal steps 36further include a pH modification step 38 through the addition of LiOH40 to raise the pH to about 9. The product of step 38 is passed to abelt filter 42 from which Al, Fe, Mn and Mg containing precipitates arerecovered. The impurity removal steps 36 further include a calciumprecipitation step 44 with the addition of either sodium carbonate (sodaash) or lithium carbonate 46, producing a calcium containing precipitate48 from a further belt filter 50.

A thickener underflow product 52 of the second thickening step 28 b ispassed to a drying step 54 before passing to waste 56 and subsequentdisposal 58.

The liquid product of the belt filter 50, being largely LiCl solution,is passed to a concentration step 60 and in turn to a fractionalcrystallisation step 62. In the concentration step 60 the LiCl solutionis concentrated to near saturation point, for example 35 to 40% LiClw/w, and is cooled to a sub zero temperature. In the subsequentfractional crystallisation step 62 Na and K impurities 64 are largelyremoved, as NaCl and KCl crystals, respectively, by filtration.

After the removal of substantially all impurities as described above,the lithium chloride solution is passed through an ion exchange step 66,comprising an Ion Exchange (IX) column 68 by which substantially all ofany residual calcium, magnesium and other multivalent cations areremoved to a level of less than about 10 ppm, for example 1 ppm.

The further purified lithium chloride solution is then heated to 90° C.and pumped to an electrolysis step 70 comprising a number ofelectrolysers, for example 6 to 20 electrolysers, in which lithiumchloride and water are consumed to produce lithium hydroxide, chlorineand hydrogen.

After passing through the electrolysers, the weak or depleted lithiumchloride solution contains dissolved chlorine gas. Before this weaklithium chloride solution is recycled to the slurrying step immediatelyprior to the leach circuit 22, the dissolved chlorine is removed in twostages. In a first stage hydrochloric acid is added to the lithiumchloride solution to reduce the pH to<5 which forces some of thechlorine gas out of solution. The remaining dissolved chlorine gas isthen removed by air stripping the solution (not shown).

Chlorine and hydrogen produced as by-products are combined to produceHCl acid which is used in the slurrying step and leaching circuit 22.

The lithium hydroxide solution obtained from the electrolysis step 70 ispassed firstly to a holding tank 72, from which it can either be (i)evaporated and crystallised to produce lithium hydroxide monohydratecrystals, or (ii) sent to carbonation step to convert into lithiumcarbonate, as clearly shown in FIG. 1.

In the first of these options, the lithium hydroxide in solution iscrystallised in, for example, a vacuum evaporative crystalliser 80 (Oslotype) operating at a temperature of about 80° C. and pressure of about45 kPa(a). The residence time is about 60 minutes so as to achieve acoarse crystal product. The resulting water vapour is recompressed,combined with make-up steam and used as the heating medium for thecrystalliser 80.

Lithium hydroxide crystals are washed by cold water (not shown)achieving a wash efficiency of 99%. The resulting wash solution isrecycled back to the leach circuit 22 as noted above. Solids from thecentrifuge are fed to an indirect-fired kiln or dryer 82, operating atabout 120° C., which dries the crystals. The crystal product, beingbattery grade LiOH.H₂O, is pneumatically conveyed to product bins 84,and cooled to 50° C. in a jacketed screw conveyer 86 as it is conveyedultimately to bagging stations (not shown).

In the second option noted above, lithium carbonate may be produced bycarbonation of lithium hydroxide solution by passing compressed carbondioxide gas 88 though the solution of lithium hydroxide in a carbonationvessel 90 in which lithium carbonate is precipitated. This slurry is fedto a washer/centrifuge 92 by way of a filter 94, after which wash wateris recycled with any remaining lithium hydroxide solution or motherliquor to electrolysis 70. Wet lithium carbonate crystals are fed to adryer 96 in which hot air is used to dry the crystals. Medium pressureair is used to heat the air. After drying the battery grade lithiumcarbonate may be micronized to a particle size requested by a customerprior to passing to storage bins 98 and subsequent bagging (not shown).

Condensate throughout the process is used as make-up water for hotprocess water, cold process water and cooling water. As the process doesnot return condensate there is an overall positive water balance andabout 1/10^(th) of the process water is discharged to a sewerage system(not shown).

It is envisaged that tantalite and alumina may also be recovered usingthe process of the present invention. The filter cake from thethickening step may be discharged to a tantalite recovery plant (notshown). Discharge from the tantalite recovery plant may be fed onto abelt filter to remove water, which is returned to the tantalite recoveryplant. The filter does not use washing and has a filtration are of 19m². The filter cake from the belt filter is dried in a direct-firedkiln. The dry alumina silicate is cooled to 50° C. in a jacketed screwconveyor and then pneumatically conveyed to a storage bin prior todispatch.

In accordance with a second embodiment of the present invention thelithium containing material may be provided in the form of a lithiumcontaining brine. Brines do not require the calcining, cooling, millingand leach steps as described for the first embodiment of the presentinvention but it is envisaged that the remainder of the process will besubstantially similar to that of the first embodiment described above.

As can be seen from the above, the process of the present inventionprovides a process by which a high purity or battery grade lithiumhydroxide and lithium carbonate products may be obtained from analpha-spodumene ore or concentrate, or from a lithium containing brine,whilst also allowing the production of a hydrogen chloride gas product.

Modifications and variations such as would be apparent to the skilledaddressee are considered to fall within the scope of the presentinvention. For example, it is envisaged that the leach circuit 22 maycomprise only a single leach stage/operation without departing from thescope of the present invention.

1. A process for the treatment of a lithium containing material, theprocess comprising the steps of: (i) Preparing a process solution fromthe lithium containing material; (ii) Passing the process solution fromstep (ii) to a series of impurity removal steps thereby providing asubstantially purified lithium chloride solution; and (iii) Passing thepurified lithium chloride solution of step (ii) to an electrolysis stepthereby producing a lithium hydroxide solution.
 2. The process of claim1, wherein the process solution of step (i) is prepared in the form of apregnant leach solution.
 3. The process of claim 2, wherein the pregnantleach solution is formed by passing a lithium containing material to aleach step in which the material is leached with hydrochloric acid. 4.The process of any one of the preceding claims, wherein the impurityremoval step (ii) further comprises a concentration step such that theprocess solution is concentrated to near saturation of lithium chloride.5. The process of any one of the preceding claims, wherein the lithiumhydroxide solution produced in step (iii) is thickened by evaporation ofwater to provide lithium hydroxide monohydrate crystals.
 6. The processof any one of the preceding claims, wherein the lithium hydroxidesolution produced in step (iii) is carbonated by passing compressedcarbon dioxide through the solution, thereby producing a lithiumcarbonate precipitate.
 7. The process of any one of the precedingclaims, wherein the lithium containing material is an alpha-spodumeneore or ore concentrate and the process further comprises a first step inwhich that alpha-spodumene ore or ore concentrate is calcined to producebeta-spodumene.
 8. The process of any one of claims 1 to 6, wherein thelithium containing material is a lithium containing brine.
 9. Theprocess of claim 6, wherein a first portion of the lithium hydroxidesolution produced in step (iii) is thickened byevaporation/crystallisation to provide lithium hydroxide monohydratecrystals and a second portion thereof is carbonated by passingcompressed carbon dioxide through the solution, thereby producing alithium carbonate precipitate.
 10. The process of any one of thepreceding claims, wherein the impurity removal steps of step (ii)include one or more of hyrdropyrolysis of Al and Fe chlorides, pHincrease to precipitate hydroxides of Al, Fe, Mg and Mn, lithiumcarbonate precipitation for removal of Ca, and fractionalcrystallisation for the removal of Na and K.
 11. The process of claim10, wherein the fractional crystallisation for the removal of Na and Kis conducted immediately after the concentration step.
 12. The processof claim 10 or 11, wherein the impurity removal steps further comprisesan ion exchange step.
 13. The process of claim 12, wherein the ionexchange step removes substantially all calcium, magnesium and othermultivalent cations remaining in the process solution.
 14. The processof claim 13, wherein such multivalent cations are removed to a level ofless than about 10 ppm.
 15. The process of claim 13 or 14, wherein suchmultivalent cations are removed to a level of about 1 ppm.
 16. Theprocess of any one of claims 9 to 15, wherein water evaporated from thesolution in evaporation/crystallisation is recompressed, combined withmake-up steam and utilised in evaporation/crystallisation.
 17. Theprocess of any one of claims 9 to 16, wherein theevaporation/crystallisation step utilises a vacuum evaporativecrystalliser.
 18. The process of any one of claims 7 to 17, wherein thebeta-spodumene is cooled and milled prior to the leach step.
 19. Theprocess of claim 18, wherein the beta-spodumene is milled to less thanabout 300 μm.
 20. The process of claim 18 or 19, wherein thebeta-spodumene is milled to a P₈₀ of about 75 μm.
 21. The process of anyone of claims 3 to 20, wherein the leach of step (ii) is conducted atelevated temperature.
 22. The process of any one of claims 3 to 21,wherein the hydrochloric acid solution used in the leach step is about20% HCl w/w.
 23. The process of claim 22, wherein the elevatedtemperature of the leach of step is about the boiling point of thehydrochloric acid solution used in the leach step.
 24. The process ofany one of claims 3 to 23, wherein the leach step is conducted atatmospheric pressure.
 25. The process of any one of claims 3 to 24,wherein the leach step is conducted in a chlorination kiln at about 108°C. over a residence time of about 6 to 10 hours.
 26. The process ofclaim 25, wherein the leach step is conducted over a residence time ofabout 8 hours.